CN102229536A - Method for separating amino alkyl alcohol through membrane electrodialysis - Google Patents
Method for separating amino alkyl alcohol through membrane electrodialysis Download PDFInfo
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- CN102229536A CN102229536A CN2011101025375A CN201110102537A CN102229536A CN 102229536 A CN102229536 A CN 102229536A CN 2011101025375 A CN2011101025375 A CN 2011101025375A CN 201110102537 A CN201110102537 A CN 201110102537A CN 102229536 A CN102229536 A CN 102229536A
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Abstract
The invention discloses a method for separating amino alkyl alcohol through membrane electrodialysis, and relates to a method for separating 2-aminopropanol from aqueous solution containing 2-aminopropanol and inorganic salt through an electrodialysis method. In the method, the aqueous solution containing 2-aminopropanol and inorganic salt is subjected to electrodialysis treatment in an electrodialysis device; the separation of 2-aminopropanol, sulphate and other inorganic salts can be realized; the disadvantages of a final treatment in the traditional solvent method are overcome; the separation energy consumption is obviously reduced; and the cost is reduced. The method disclosed by the invention has the benefits which are mainly embodied in that: salt is removed by using an electrodialysis technology; the separation of 2-aminopropanol, sulphate and other inorganic salts can be realized; the traditional method for separating by using an organic solvent is replaced; the recovery rate of 2-aminopropanol is improved; salt is removed by using the electrodialysis technology; the energy consumption in the purification process of a product can be obviously reduced; a lot of flammable and toxic organic solvents of methanol, ethanol and the like can be prevented from being adopted; both the production cost and the emission of the three wastes (waste gas, waste water and industrial residue) can be greatly reduced; the product quality is further improved; and a by-product of sodium sulphate in high quality can be obtained.
Description
Technical field
The present invention relates to the method that a kind of embrane method electrodialysis separates purification aminoalkyl group alcohol, be specifically related to use cationic exchange membrane and anion-exchange membrane, arrange by different order, form the ionic membrane electrodialysis unit, from the aqueous solution of aminoalkyl group alcohol and inorganic salt, separate amino alkyl alcohol.
Background technology
The 2-aminopropanol is the key intermediate of synthesising bacteria anti-reflecting medicine Ofloxacine USP 23, and there are three kinds of chiral isomers in the 2-aminopropanol by its sterie configuration difference: the L-2-aminopropanol; The D-2-aminopropanol; The DL-2-aminopropanol.Wherein the L-2-aminopropanol is the key intermediate of synthetic Levofloxacin, the DL-2-aminopropanol is the key intermediate of synthetic Ofloxacine USP 23, Ofloxacine USP 23 and Levofloxacin are the essential drugses of China, the height of its production cost and quality fine or not extremely important.
It is method and the catalyst system therefor and the Preparation of catalysts method of feedstock production α-An Jichun with the a-amino acid that patent ZL200810126200.6 has reported a kind of, and is successfully applied to the industrialization of L-2-aminopropanol, D-2-aminopropanol, DL-2-aminopropanol.The technological breakthrough of shortening single stage method synthesizing amino propyl alcohol reduces production cost of products significantly, quality product further improves, and realized cleaner production truly, for promoting the state of the art of (left side) Ofloxacine USP 23 whole industry chain, reduce cost, strengthen (left side) Ofloxacine USP 23 product competitiveness and lay a good foundation.
Use the synthetic technology of patent ZL200810126200.6 invention, the 2-L-Ala by hydrogen reducing, obtains the 2-aminopropanol under catalyst action, and its chemical equation is as follows:
After finishing, reaction obtains the acidic solution of 2-aminopropanol.For obtaining the finished product, aminopropanol be purified from mixed aqueous solution, traditional separating and purifying method is reaction solution to be neutralized evaporation concentration with alkali earlier; By adding the solvents miscible such as methyl alcohol, ethanol, the trimethyl carbinol, separate out inorganic salt with water; Inorganic salt are told in filtration, obtain solution elder generation distillating recovering solvent, and rectifying obtains product again.Find in the production process that there is following shortcoming in this post-treating method:
(1) a large amount of mother liquors of aftertreatment need rectifying, and steam consumption is big, and product per ton needs 9～12 tons of steam;
(2) use organic solvents such as a large amount of methyl alcohol, ethanol, the trimethyl carbinol, organic solvent is difficult to reclaim fully, and a part enters inorganic salt, and it is residual that a part enters rectifying still, causes environmental pollution; Solvent is volatile in addition, and the solvent loss amount is big during summer, has increased production hidden danger, and production cost rises;
(3) add the separated from solvent inorganic salt in the aqueous solution of aminopropanol and salt, separation efficiency is low.Inorganic salt are separated out in the still-process, stick to the still kettle wall, and influence is conducted heat, and inorganic salt corrodibility is strong simultaneously, rectifying tower requirement for anticorrosion height, and investment is big, and the upkeep cost height is produced unstable;
(4) inorganic salt that contain solvent of by-product are difficult to recycle.
Summary of the invention
At the deficiency that above-mentioned saliferous 2-aminopropanol aqueous solution solvent method aftertreatment technology exists, the purpose of this invention is to provide a kind of method of utilizing the electrodialysis isolation technique to separate the 2-aminopropanol.
Concrete technological method of the present invention is as follows:
(1) separation solution preparation
The 2-aminopropanol is prepared by the technology of patent ZL200810126200.6 invention.The 2-L-Ala by hydrogen reducing, obtains the acidic aqueous solution of aminopropanol under catalyst action, isolate catalyzer after, this aqueous solution (abbreviating hydrogenation reaction solution as) mainly consist of 2-aminopropanol (wt%) 6%～20%, [SO
4 2-] (wt%) 5%～15%, [H
2PO
4 -] (wt%) 1%～5%, impurity 1.0～3.0%, all the other are water, pH value of solution is 2-5.Impurity is small molecules resolvent and the unreacted raw material in the alanine catalytic hydrogenation reaction process, separable removing in rectifying.
(2) preparation neutralizer
Hydrogenation reaction solution is regulated pH to 7-12 with 30% sodium hydroxide solution earlier, and the aqueous solution specific conductivity that obtains is neutralizer at 120ms/cm～200ms/cm hereinafter to be referred as it, and neutralizer carries out electrodialysis process.
(3) electrodialysis unit
Electrodialysis unit can be by commercially available acquisition, and the film of electrodialysis process device is an ion-exchange membrane, and area 200mm * 400mm, selected cationic exchange membrane and anion-exchange membrane are heterogeneous membrane or homogeneous membrane, and its operation is undertaken by the specification sheets of film and device.
In the method provided by the invention, for improving the efficient of electrodialysis process, electrodialysis unit is spaced by cationic exchange membrane and anion-exchange membrane, forms the ionic membrane electrodialysis unit of 2 cell structure; Be combined as one section of one-level or one-level multistage (secondary or more than the secondary) by the separate unit electrodialysis unit, can make serial or parallel connection between every grade.
(4) one sections electrodialysis
Neutralizer is squeezed into diluting compartment with pump, keep diluting compartment pressure 0.02MPa～0.03MPa; The concentration compartments squeezes into tap water or the pure water that specific conductivity is 20～200 μ s/cm with pump, keeps the pressure 0.02MPa～0.03MPa of concentration compartments.Begin energising, operating voltage is that 20V～60V, current density are 1mA/cm
2～100mA/cm
2, the feed liquid flow velocity is 0.1cm/s～30cm/s in the compartment, service temperature is 5 ℃～60 ℃.Chamber to be diluted neutralizer specific conductivity is reduced to 20000～30000 μ s/cm, and diluting compartment obtains demineralised liquid one time, and the electrical conductivity of solution of concentration compartments is called strong brine one time at 100ms/cm～180ms/cm.
(5) two sections electrodialysis
A strong brine is discharged the concentration compartments, changing specific conductivity is tap water or the pure water of 20 μ s/cm～200 μ s/cm, continuation is carried out electrodialytic desalting to a demineralised liquid of diluting compartment, the feed liquid specific conductivity of chamber to be diluted is reduced to below the 2000 μ s/cm, stop energising, diluting compartment obtains the secondary demineralised liquid, and the solution of the specific conductivity 20ms/cm that the concentration compartments obtains～30ms/cm becomes the secondary strong brine.
(6) product separation
The secondary demineralised liquid obtains product 2-aminopropanol successively through dehydration by evaporation, rectifying.
Strong brine and secondary strong brine mix, monitoring, and 2-aminopropanol concentration (wt%) 0.05%～0.1%, COD1000～5000mg/L enters sewage works.
Utilize the present invention, 2-aminopropanol neutralizer adopts electrodialytic desalting, organic solvent is got rid of in aftertreatment, the serious ethanol volatile emission of having avoided using a large amount of ethanol and having caused is polluted and the production insecurity, and 2-aminopropanol rate of recovery height, reach 96～98%, product is monitored through gas-chromatography, and content reaches more than 99.8%; Compare with the solvent method desalination, energy consumption reduces more than 50%, and production cost reduces by 15～25%, has reduced three waste discharge.
In sum, the present invention prepares the 2-aminopropanol aqueous solution with the technology that electroosmose process separates patent ZL200810126200.6 invention, has fundamentally overcome the deficiency of traditional solvent aftertreatment, and organic solvent has been got rid of in aftertreatment, energy consumption significantly descends, and cost reduces.
Description of drawings
Fig. 1 is an electroosmose process 2-aminopropanol desalinating process flow process of the present invention;
Fig. 2 is the structure iron of two compartment ionic membrane electrodialysis tripping devices.
Embodiment
Embodiment 1:
Adopt the ionic membrane electrodialysis tripping device of two cell structure, the area of every film is 200mm * 400mm, and totally 40 pairs of yin, yang ion-exchange membranees are formed membrane stack.18 liters of neutralizers (are consisted of DL-2 aminopropanol (wt%) 12%, [SO
4 2-] (wt%) 8%, [H
2PO
4 -] (wt%) 4%, impurity 3.0%, pH is 7) filter pair compartment electrodialysis units are squeezed in the back with pump diluting compartment through accurate filter, in the concentration compartments, add tap water (specific conductivity is about 200 μ s/cm), utmost point water is 3% metabisulfite solution, and the current density of control ionic membrane electrodialysis tripping device is 12.5mA/cm
2, the feed liquid flow is 500L/h in diluting compartment and the concentration compartments, and temperature is 35～40 ℃.When the specific conductivity of diluting compartment reaches 18000～20000 μ s/cm, discharge a strong brine of concentration compartments, again add tap water then, proceed desalination, when the specific conductivity of diluting compartment feed liquid reaches 1800～2000 μ s/cm when following, stop energising, the 2-aminopropanol solution of diluting compartment is carried out rectifying concentrate and obtain 2-aminopropanol 2.0kg, the yield of DL-2-aminopropanol is 92.3%, GC purity assay 99.8%.10 liters of secondary strong brines.
Embodiment 2:
Adopt the ionic membrane electrodialysis tripping device of two cell structure, the area of every film is 200mm * 400mm, and totally 60 pairs of yin, yang ion-exchange membranees are formed membrane stack.18 liters of neutralizers (are consisted of aminopropanol (wt%) 12%, [SO
4 2-] (wt%) 8%, [H
2PO
4 -] (wt%) 4%, impurity 3.0%, pH is 7) filter pair compartment electrodialysis units are squeezed in the back with pump diluting compartment through accurate filter, in the concentration compartments, add tap water (specific conductivity is about 200 μ s/cm), utmost point water is 3% metabisulfite solution, and the current density of control ionic membrane electrodialysis tripping device is 12.5mA/cm
2, the feed liquid flow is 400L/h in diluting compartment and the concentration compartments, and temperature is 30～35 ℃.When the specific conductivity of diluting compartment reaches 15000～18000 μ s/cm, discharge a strong brine of concentration compartments, again add tap water then, proceed desalination, when the specific conductivity of diluting compartment feed liquid reaches 1200～1500 μ s/cm when following, stop energising, the 2-aminopropanol solution of diluting compartment is carried out rectifying concentrate and obtain 2-aminopropanol 2.1kg, the yield of 2-aminopropanol is 95.3%, GC purity assay 99.8%.10.5 liters of secondary strong brines.
Embodiment 3:
On the basis of embodiment 1, the current density of control ionic membrane electrodialysis tripping device is 8mA/cm
2, the feed liquid flow is 450L/h in the compartment, temperature is 25-30 ℃.When the specific conductivity of diluting compartment reaches 20000～25000 μ s/cm, discharge a strong brine of concentration compartments, again add tap water then, proceed desalination, when the specific conductivity of diluting compartment feed liquid reaches 1800～2000 μ s/cm when following, stop energising, the 2-aminopropanol solution of diluting compartment is carried out rectifying concentrate and obtain 2-aminopropanol 2.0kg, the yield of 2-aminopropanol is 92.0%, GC purity assay 99.8%.
Embodiment 4:
On the basis of embodiment 2, adopt the ionic membrane electrodialysis tripping device of two cell structure, the area of every film is 200mm * 400mm, totally 120 pairs of yin, yang ion-exchange membranees are formed membrane stack.15 liters of neutralizers (are consisted of L-2-aminopropanol (wt%) 12%, [SO
4 2-] (wt%) 8%, [H
2PO
4 -] (wt%) 4%, impurity (wt%) 3.0%, pH is 7) filter pair compartment electrodialysis units are squeezed in the back with pump diluting compartment through accurate filter, in the concentration compartments, add tap water (specific conductivity is about 200 μ s/cm), utmost point water is 3% metabisulfite solution, and the current density of control ionic membrane electrodialysis tripping device is 12.5mA/cm
2, the feed liquid flow is 600L/h in diluting compartment and the concentration compartments, and temperature is 30～35 ℃.When the specific conductivity of diluting compartment reaches 12000～16000 μ s/cm, discharge a strong brine of concentration compartments, again add tap water then, proceed desalination, when the specific conductivity of diluting compartment feed liquid reaches 1300～1600 μ s/cm when following, stop energising, the L-2-aminopropanol solution of diluting compartment is carried out rectifying concentrate and obtain 2-aminopropanol 1.7kg, the yield of 2-aminopropanol is 96.3%, GC purity assay 99.8%.8.5 liters of secondary strong brines.
Claims (6)
1. the post-treating method of a 2-aminopropanol aqueous solution, wherein, the 2-aminopropanol aqueous solution consist of 2-aminopropanol (wt%) 6%～20%, [SO
4 2-] (wt%) 5%～15%, [H
2PO
4 -] (wt%) 0%～5%, impurity 1.0～3.0%, all the other are water, Na
+, pH value of solution is 2-5.The 2-aminopropanol aqueous solution is neutralized to pH6-9 with sodium hydroxide, obtains 2-aminopropanol neutralizer, and specific conductivity is 120ms/cm～200ms/cm, further handles with electrodialytic method.Neutralizer is squeezed into the electrodialysis unit diluting compartment with pump, keep diluting compartment pressure 0.02MPa～0.03MPa; The concentration compartments squeezes into tap water or the pure water that specific conductivity is 20～200 μ s/cm with pump, keeps the pressure 0.02MPa～0.03MPa of concentration compartments.Begin energising, operating voltage is 20V～60V, and current density is 1mA/cm
2～100mA/cm
2, the feed liquid flow velocity is 200L/h～1500L/h in the compartment, service temperature is 5 ℃～60 ℃.Chamber to be diluted neutralizer specific conductivity is reduced to 20000～30000 μ s/cm, a strong brine is discharged the concentration compartments, changing specific conductivity is tap water or the pure water of 20 μ s/cm～200 μ s/cm, continuation is carried out electrodialytic desalting to a demineralised liquid of diluting compartment, the feed liquid specific conductivity of chamber to be diluted is reduced to below the 2000 μ s/cm, stop energising, diluting compartment obtains the secondary demineralised liquid, the secondary strong brine of the specific conductivity 20ms/cm that the concentration compartments obtains～30ms/cm.The secondary demineralised liquid obtains product 2-aminopropanol successively through dehydration by evaporation, rectifying.
2. method according to claim 1,2-aminopropanol solution consist of 2-aminopropanol (wt%) 6%～20%, [SO
4 2-] (wt%) 5%～15%, [H
2PO
4 -] (wt%) 0%～5%, impurity (wt%) 1.0～3.0%, all the other are water, pH value of solution is 2-5.
3. according to claim 1 and 2 described methods, the 2-aminopropanol aqueous solution separates 2-aminopropanol and inorganic salt with electrodialytic method after neutralizing.
4. method according to claim 1, used cationic exchange membrane of the electrodialysis unit of 2-aminopropanol and anion-exchange membrane are out-phase or homogeneous ion-exchange membrane, cationic exchange membrane and anion-exchange membrane are spaced, the ionic membrane electrodialysis unit of forming 2 cell structure, but separate unit electrodialysis unit serial or parallel connection is combined as one section of one-level or multistage multistage.
5. method according to claim 1, electrodialytic operating parameters are the pressure 0.02MPa～0.03MPa of concentration compartments.Begin energising, operating voltage is 20V～60V, and current density is 1mA/cm
2～100mA/cm
2, the feed liquid flow velocity is 200L/h～1500L/h in the compartment, service temperature is 5 ℃～60 ℃.
6. method according to claim 1, the 2-aminopropanol comprises the L-2-aminopropanol, D-2-aminopropanol and DL-2-aminopropanol.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102584606A (en) * | 2011-12-28 | 2012-07-18 | 浙江工业大学 | Method for preparing aminopropanol by bipolar membrane electrodialysis |
| CN105622435A (en) * | 2016-02-16 | 2016-06-01 | 建德蓝忻环境科技有限公司 | Bipolar membrane device for preparing amino-1-propanol |
| CN109809964A (en) * | 2019-03-04 | 2019-05-28 | 中国科学技术大学 | A method of neopentyl glycol is purified using bipolar membrane electrodialysis system |
| CN110694479A (en) * | 2019-10-31 | 2020-01-17 | 山东益丰生化环保股份有限公司 | Purification method of cyanamide solution |
| CN112142609A (en) * | 2019-06-28 | 2020-12-29 | 浙江工业大学 | Preparation method of (D) -2-aminobutanol or (L) -2-aminobutanol |
| CN112657339A (en) * | 2019-10-15 | 2021-04-16 | 中国石油化工股份有限公司 | Electrodialysis device, electrodialysis system, and method for purifying glycolic acid raw material |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109809964A (en) * | 2019-03-04 | 2019-05-28 | 中国科学技术大学 | A method of neopentyl glycol is purified using bipolar membrane electrodialysis system |
| CN112142609A (en) * | 2019-06-28 | 2020-12-29 | 浙江工业大学 | Preparation method of (D) -2-aminobutanol or (L) -2-aminobutanol |
| CN112142609B (en) * | 2019-06-28 | 2022-12-09 | 浙江工业大学 | Preparation method of (D) -2-aminobutanol or (L) -2-aminobutanol |
| CN112657339A (en) * | 2019-10-15 | 2021-04-16 | 中国石油化工股份有限公司 | Electrodialysis device, electrodialysis system, and method for purifying glycolic acid raw material |
| CN110694479A (en) * | 2019-10-31 | 2020-01-17 | 山东益丰生化环保股份有限公司 | Purification method of cyanamide solution |
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